CA1234291A - Recovery of gold from auriferous refractory iron- containing sulphidic material - Google Patents
Recovery of gold from auriferous refractory iron- containing sulphidic materialInfo
- Publication number
- CA1234291A CA1234291A CA000464183A CA464183A CA1234291A CA 1234291 A CA1234291 A CA 1234291A CA 000464183 A CA000464183 A CA 000464183A CA 464183 A CA464183 A CA 464183A CA 1234291 A CA1234291 A CA 1234291A
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- Prior art keywords
- gold
- slurry
- pulp density
- process according
- solids
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Classifications
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- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/04—Obtaining noble metals by wet processes
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B11/00—Obtaining noble metals
- C22B11/08—Obtaining noble metals by cyaniding
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE
A process for recovering gold from refractory auriferous iron containing sulphidic material which comprises treating an aqueous slurry of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250°C under a total pressure of from about 500 to about 5000 kPa to oxidize sulphide sulphur to sulphate form and release gold from a refractory state. The pH of the result-ant oxidized slurry is adjusted to a value suitable for cyani-dation. The pH adjusted slurry is subjected to a cyanidation step in which gold is dissolved in a cyanide solution. The cyanided slurry is diluted to a pulp density in the range of from about 2 to about 10% solids by weight. The diluted slurry is subjected to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and gold from the gold-containing solution and from the high pulp density gold-containing slurry is separately recovered.
A process for recovering gold from refractory auriferous iron containing sulphidic material which comprises treating an aqueous slurry of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250°C under a total pressure of from about 500 to about 5000 kPa to oxidize sulphide sulphur to sulphate form and release gold from a refractory state. The pH of the result-ant oxidized slurry is adjusted to a value suitable for cyani-dation. The pH adjusted slurry is subjected to a cyanidation step in which gold is dissolved in a cyanide solution. The cyanided slurry is diluted to a pulp density in the range of from about 2 to about 10% solids by weight. The diluted slurry is subjected to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and gold from the gold-containing solution and from the high pulp density gold-containing slurry is separately recovered.
Description
Lo This invention relates to the recovery of gold from refractory airfares iron-contalning sulphidic material, which may for example be ore or concentrate.
It is known that it is desirable to subject refract tory airfares iron-containing sulphidic material to a pros-sure oxidation step to release gold from a refractory state before recovering gold by cyanidation, see for example United States patent No. 2,777,764 medley et at) issued January 15, 1957. Retention times normally used in conventional cyanide-lion practice are generally around 24 hours to ensure good gold recovery, although they may be from about 12 to 72 hours de-pending on the nature of the feed solids.
The present invention is based on the discovery that, after pressure oxidation treatment, the gold content of refract tory airfares iron-containing sulphidic material (usually comprising arsenopyrite and/or pyrites responds rapidly to extraction by cyanidation. In some cases, it has been found that up to about 96% of the extractable gold may be extracted by cyanida-tion in 1 hour or less, and sometimes in half an hour or less. Further, after such rapid cyanidation, the present invention utilizes the discovery that gold can be efficiently removed from the cyanide slurry by diluting the slurry to a relatively low pulp density, subjecting the diluted slurry to a liquid solids separation step to produce a gold-containing solution and a relatively high pulp den-sty slurry, and separately recovering gold from the gold-containing solution and the high pulp density slurry.
The present invention accordingly provides a process for recovering gold from refractory airfares iron-contain-in sulphidic material comprising treating an aqueous slurry ~234~1 of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250C, preferably from about 160 to about 200C, under a total pressure of from about 500 to about 5000 spa to oxidize sulfide Selfware to sulfite form and release gold from a refractory state, adjust-in the pi of the resultant oxidized slurry to a value suitable for cyanidation, subjecting the pi adjusted slurry to a cyan-ration solution, diluting the cyanide slurry to a pulp den-sty in the range of from about 2 to about 10% solids by weight, subjecting the diluted slurry to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and separately no-covering gold from the gold-containing solution and from the high pulp density gold-contalning slurry.
Advantageously, the oxidized slurry is washed prior to the pi adjustment step to remove soluble iron, arsenic, and sulfite.
Gold may be recovered from the gold containing soul-lion by adsorption by activated carbon or by an ion exchange ZOO resin. Gold may be recovered from the high pulp density slurry by adsorption by activated carbon in a carbon in leach or carbon in pulp circuit.
The relatively high pulp density gold-containing slurry may have a pulp density in the range of from about 45 to about 60% solids by weight or preferably from about 35 to about 45%.
One embodiment of the invention will now be described by way of example, with reference to the accompanying drawing which shows a schematic flow diagram of a process for recover-in gold from a refractory airfares iron-containing sulk phidic material.
~23~
Referring to the drawing, the refractory auriferousiron-containlng sulphidic material to be treated will usually contain arsenopyrite and/or pyrites and the ore or a suitable concentrate may be treated. The ore or concentrate is ground to about 80% less than 200 mesh and supplied as an aqueous slurry to a pressure oxidation step 12 where the material is treated at a temperature of from about 16Q to about 200C
under a total pressure of from about Tao about 5000 spa to oxidize substantially all the sulfite Selfware to sulfite form and liberate gold from the refractory step. During the pressure oxidation step, the solids undergo further size reduction, particularly sulfides containing refractory gold.
The sulfides are substantially completely destroyed during the oxidation since the arsenic, iron and Selfware are dissolved.
A significant portion of the arsenic and iron, and to a lesser extent the Selfware (as sulfite), may substantially be precipitated but such solids are extremely fine and are prows-pitted externally to the gold particles, rendering the gold more easily recoverable.
The hot oxidized slurry passes to the first stage of a two-stage countercurrent recantation washing step comprise in a first stage 14, first stage thickener 16, second stage 18, and second stage thickener 20. In the first stage 14, the hot oxidized slurry is washed with overflow from the second stage thickener 18, and the washed slurry passes to the first stage thickener 16 from which used wash water is removed as overflow.
The washed solids are recovered as under flow and passed to the second wash stage 18 where fresh wash water is added. The washed slurry passes to the second stage thickener 20 from which wash water removed as overflow is recycled to the first wash stage ~2342S~
14 as previously mentioned, with washed solids being removed as under flow.
This washing step removes soluble iron, arsenic and sulfite, thereby reducing lime requirements and the likelihood of slime precipitation in the subsequent pi adjust-mint step to be described, and also removes sinusoids fib-crated in the pressure oxidation step 12. The washing step also serves to reduce the temperature of the slurry to a temperature in the range of from about 40 to about 70C.
The washed, thickened slurry then proceeds to pi adjustment step 22 where lime is added to raise the pi of the slurry to a value suitable for cyanidation, usually in the range of from about 9 to about 11, for example about 10.5.
The pi adjustment slurry is then subjected to a single stage or possible two stage cyanidation step 24. In ; accordance with the invention, retention time is short, and the vessel or vessels used may be considerably smaller than in conventional practice. Also, the vessel or vessels may be closed to take advantage of improved cyanidation leach rates at elevated temperatures without incurring undesirable loss of cyanide as vapour. Conventional cyanidation is carried out at ambient temperatures, usually 20 to 35C for this reason. Air requirements are minimal and air sparring may not be required, further lowering cyanide loss. As mentioned above, the bulk of the sinusoids were removed in the wash stages 14, 18. The cyanidation may be conducted in stirred tanks or in a tube reactor at higher pulp densities than are possible in conventional stirred tanks.
::~23~9~
After the cyanidation step 24, the slurry passes to a dilution step 26 where the slurry is cooled and diluted to less than about 10~ solids by weight, and preferably to less than about 5% solids with barren cyanide solution from a gold recovery step to be described later. The diluted slurry then proceeds to a thickener 28, from which the overflow contain-in a major proportion of the feed gold is passed to a cool-in step 30 and then to a gold recovery step 32.
In the gold recovery step 32, the gold-containing solution is passed through a column or a series of beds containing activated carbon or ion exchange resin which adsorbs gold. The gold depleted cyanide solution from the gold recovery step 32 is utilized in the slurry dilution step 26. The preliminary cooling step 30 serves to enhance the loading characteristics of the gold onto the activated carbon or ion exchange resin in the gold recovery step 32, and also results in a cooler barren cyanide solution which consequently effects cooling in the slurry dilution step 26.
This also produces advantageous cooling for the subsequent carbon in leach circuit to be described.
The dilution step 26 is in fact a wash/repulp step, at a high wash ratio, thereby enabling recovery of the major portion of the dissolved gold in the primary recovery step 32.
The heavy dilution of the cyanide slurry in the dilution step 26 results in improved flocculation in the thickener 28, reduce in thickener requirements and enabling slurry under flow con-twining from about 45 to 60~ solids to be readily achieved.
The under flow from the thickener 28 is diluted in repulsing step 34 with Warren cyanide solution from the carbon in leach step to be described, to a pulp density in the range ~L~3~2~
of from about 35 to about 45% solids by weight, providing further cooling.
The diluted under flow slurry is then processed through a carbon in leach circuit 36 having from about 4 to 8 stages for the recovery of the remaining soluble gold, the gold which has been adsorbed by residue slimes, and additional leaching and adsorption of unextracted gold. Thus, there may be one or two cyanidation leaching stages followed by up to 7 stages which contain carbon. The retention times and/or the number of stages in the carbon in leach circuit 36 can be greatly reduced compared to conventional practice since the character-sties of the solids being treated favor more rapid leaching of the gold and since the major portion of the recoverable gold has been removed as overflow from the thickener 28. Barren slurry from the carbon in leach circuit 36 is thickened prior to disposal for recovery of cyanide bearing solution for recycle to repulsing step 34.
It will be noted that only the carbon utilized in the carbon in leach circuit 36 is contacted with slurry, there-by minimizing the fouling of carbon by residue fines and slimes with the result that carbon regeneration or cleaning (for example by acid washing and/or thermal reactivation) require-mints are reduced. The carbon (and/or ion exchange resin) used in the gold recovery step 32 is less subject to fouling by slimes and loading with contaminants, since most of the common impurities have been removed in the pressure oxide-lion and wash steps 12, 14, 18. This makes is possible to achieve relatively high gold loadings on the carbon in the gold recovery step 32, so that direct smelting or burning of the loaded carbon becomes an economically attractive ~Z3~
alternative to stripping and electrowinning or zinc precipi-station of the gold from the stripped solution followed by regeneration of carbon.
An example of the invention will now be described.
EXAMPLE
A refractory airfares iron-containing sulphidic concentrate contained 228 g/t A, 41 g/t A and by weight 7.0% As, 24.7% Fe and 18% S, The concentrate was pressure oxidized at a pulp density of about 16% under a total pressure of 1475 spa at a temperature of 185C with a retention time of 2 hours. The autoclave discharge slurry proceeded through 2 stages of countercurrent recantation washing.
The thickened washed oxidized solids were then fed as a slurry with a pulp density of about 51% solids to a pi adjustment step where the slurry was limed through about pi 11 and diluted to 35 to I solids.
The pi adjusted slurry was then leached with sodium cyanide solution from about 4 h, and the cyanide slurry diluted to a pulp density of about 2.5% solids by weight with barren solution from a gold recovery step. The diluted slurry was thickened, with the under flow being in the 45 to 51% solids range. The gold was recovered from the overflow by carbon adsorption, with subsequent stripping by NaCN/NaOH solution and cementation of gold and silver with zinc dust. The under flow slurry was diluted to about 30%
solids by recycle, and gold was recovered in the carbon in leach step. It was found that about 94.5% of the extract-able gold was recovered from the thickener overflow in the gold recovery step, with the remaining 5.5% being recovered from the thickener under flow in the carbon in leach step.
~23g~9~
Other examples and embodiments will be readily apparent to a person skilled in the art, the scope of the invention being defined in the appended claims.
:
:
It is known that it is desirable to subject refract tory airfares iron-containing sulphidic material to a pros-sure oxidation step to release gold from a refractory state before recovering gold by cyanidation, see for example United States patent No. 2,777,764 medley et at) issued January 15, 1957. Retention times normally used in conventional cyanide-lion practice are generally around 24 hours to ensure good gold recovery, although they may be from about 12 to 72 hours de-pending on the nature of the feed solids.
The present invention is based on the discovery that, after pressure oxidation treatment, the gold content of refract tory airfares iron-containing sulphidic material (usually comprising arsenopyrite and/or pyrites responds rapidly to extraction by cyanidation. In some cases, it has been found that up to about 96% of the extractable gold may be extracted by cyanida-tion in 1 hour or less, and sometimes in half an hour or less. Further, after such rapid cyanidation, the present invention utilizes the discovery that gold can be efficiently removed from the cyanide slurry by diluting the slurry to a relatively low pulp density, subjecting the diluted slurry to a liquid solids separation step to produce a gold-containing solution and a relatively high pulp den-sty slurry, and separately recovering gold from the gold-containing solution and the high pulp density slurry.
The present invention accordingly provides a process for recovering gold from refractory airfares iron-contain-in sulphidic material comprising treating an aqueous slurry ~234~1 of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250C, preferably from about 160 to about 200C, under a total pressure of from about 500 to about 5000 spa to oxidize sulfide Selfware to sulfite form and release gold from a refractory state, adjust-in the pi of the resultant oxidized slurry to a value suitable for cyanidation, subjecting the pi adjusted slurry to a cyan-ration solution, diluting the cyanide slurry to a pulp den-sty in the range of from about 2 to about 10% solids by weight, subjecting the diluted slurry to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and separately no-covering gold from the gold-containing solution and from the high pulp density gold-contalning slurry.
Advantageously, the oxidized slurry is washed prior to the pi adjustment step to remove soluble iron, arsenic, and sulfite.
Gold may be recovered from the gold containing soul-lion by adsorption by activated carbon or by an ion exchange ZOO resin. Gold may be recovered from the high pulp density slurry by adsorption by activated carbon in a carbon in leach or carbon in pulp circuit.
The relatively high pulp density gold-containing slurry may have a pulp density in the range of from about 45 to about 60% solids by weight or preferably from about 35 to about 45%.
One embodiment of the invention will now be described by way of example, with reference to the accompanying drawing which shows a schematic flow diagram of a process for recover-in gold from a refractory airfares iron-containing sulk phidic material.
~23~
Referring to the drawing, the refractory auriferousiron-containlng sulphidic material to be treated will usually contain arsenopyrite and/or pyrites and the ore or a suitable concentrate may be treated. The ore or concentrate is ground to about 80% less than 200 mesh and supplied as an aqueous slurry to a pressure oxidation step 12 where the material is treated at a temperature of from about 16Q to about 200C
under a total pressure of from about Tao about 5000 spa to oxidize substantially all the sulfite Selfware to sulfite form and liberate gold from the refractory step. During the pressure oxidation step, the solids undergo further size reduction, particularly sulfides containing refractory gold.
The sulfides are substantially completely destroyed during the oxidation since the arsenic, iron and Selfware are dissolved.
A significant portion of the arsenic and iron, and to a lesser extent the Selfware (as sulfite), may substantially be precipitated but such solids are extremely fine and are prows-pitted externally to the gold particles, rendering the gold more easily recoverable.
The hot oxidized slurry passes to the first stage of a two-stage countercurrent recantation washing step comprise in a first stage 14, first stage thickener 16, second stage 18, and second stage thickener 20. In the first stage 14, the hot oxidized slurry is washed with overflow from the second stage thickener 18, and the washed slurry passes to the first stage thickener 16 from which used wash water is removed as overflow.
The washed solids are recovered as under flow and passed to the second wash stage 18 where fresh wash water is added. The washed slurry passes to the second stage thickener 20 from which wash water removed as overflow is recycled to the first wash stage ~2342S~
14 as previously mentioned, with washed solids being removed as under flow.
This washing step removes soluble iron, arsenic and sulfite, thereby reducing lime requirements and the likelihood of slime precipitation in the subsequent pi adjust-mint step to be described, and also removes sinusoids fib-crated in the pressure oxidation step 12. The washing step also serves to reduce the temperature of the slurry to a temperature in the range of from about 40 to about 70C.
The washed, thickened slurry then proceeds to pi adjustment step 22 where lime is added to raise the pi of the slurry to a value suitable for cyanidation, usually in the range of from about 9 to about 11, for example about 10.5.
The pi adjustment slurry is then subjected to a single stage or possible two stage cyanidation step 24. In ; accordance with the invention, retention time is short, and the vessel or vessels used may be considerably smaller than in conventional practice. Also, the vessel or vessels may be closed to take advantage of improved cyanidation leach rates at elevated temperatures without incurring undesirable loss of cyanide as vapour. Conventional cyanidation is carried out at ambient temperatures, usually 20 to 35C for this reason. Air requirements are minimal and air sparring may not be required, further lowering cyanide loss. As mentioned above, the bulk of the sinusoids were removed in the wash stages 14, 18. The cyanidation may be conducted in stirred tanks or in a tube reactor at higher pulp densities than are possible in conventional stirred tanks.
::~23~9~
After the cyanidation step 24, the slurry passes to a dilution step 26 where the slurry is cooled and diluted to less than about 10~ solids by weight, and preferably to less than about 5% solids with barren cyanide solution from a gold recovery step to be described later. The diluted slurry then proceeds to a thickener 28, from which the overflow contain-in a major proportion of the feed gold is passed to a cool-in step 30 and then to a gold recovery step 32.
In the gold recovery step 32, the gold-containing solution is passed through a column or a series of beds containing activated carbon or ion exchange resin which adsorbs gold. The gold depleted cyanide solution from the gold recovery step 32 is utilized in the slurry dilution step 26. The preliminary cooling step 30 serves to enhance the loading characteristics of the gold onto the activated carbon or ion exchange resin in the gold recovery step 32, and also results in a cooler barren cyanide solution which consequently effects cooling in the slurry dilution step 26.
This also produces advantageous cooling for the subsequent carbon in leach circuit to be described.
The dilution step 26 is in fact a wash/repulp step, at a high wash ratio, thereby enabling recovery of the major portion of the dissolved gold in the primary recovery step 32.
The heavy dilution of the cyanide slurry in the dilution step 26 results in improved flocculation in the thickener 28, reduce in thickener requirements and enabling slurry under flow con-twining from about 45 to 60~ solids to be readily achieved.
The under flow from the thickener 28 is diluted in repulsing step 34 with Warren cyanide solution from the carbon in leach step to be described, to a pulp density in the range ~L~3~2~
of from about 35 to about 45% solids by weight, providing further cooling.
The diluted under flow slurry is then processed through a carbon in leach circuit 36 having from about 4 to 8 stages for the recovery of the remaining soluble gold, the gold which has been adsorbed by residue slimes, and additional leaching and adsorption of unextracted gold. Thus, there may be one or two cyanidation leaching stages followed by up to 7 stages which contain carbon. The retention times and/or the number of stages in the carbon in leach circuit 36 can be greatly reduced compared to conventional practice since the character-sties of the solids being treated favor more rapid leaching of the gold and since the major portion of the recoverable gold has been removed as overflow from the thickener 28. Barren slurry from the carbon in leach circuit 36 is thickened prior to disposal for recovery of cyanide bearing solution for recycle to repulsing step 34.
It will be noted that only the carbon utilized in the carbon in leach circuit 36 is contacted with slurry, there-by minimizing the fouling of carbon by residue fines and slimes with the result that carbon regeneration or cleaning (for example by acid washing and/or thermal reactivation) require-mints are reduced. The carbon (and/or ion exchange resin) used in the gold recovery step 32 is less subject to fouling by slimes and loading with contaminants, since most of the common impurities have been removed in the pressure oxide-lion and wash steps 12, 14, 18. This makes is possible to achieve relatively high gold loadings on the carbon in the gold recovery step 32, so that direct smelting or burning of the loaded carbon becomes an economically attractive ~Z3~
alternative to stripping and electrowinning or zinc precipi-station of the gold from the stripped solution followed by regeneration of carbon.
An example of the invention will now be described.
EXAMPLE
A refractory airfares iron-containing sulphidic concentrate contained 228 g/t A, 41 g/t A and by weight 7.0% As, 24.7% Fe and 18% S, The concentrate was pressure oxidized at a pulp density of about 16% under a total pressure of 1475 spa at a temperature of 185C with a retention time of 2 hours. The autoclave discharge slurry proceeded through 2 stages of countercurrent recantation washing.
The thickened washed oxidized solids were then fed as a slurry with a pulp density of about 51% solids to a pi adjustment step where the slurry was limed through about pi 11 and diluted to 35 to I solids.
The pi adjusted slurry was then leached with sodium cyanide solution from about 4 h, and the cyanide slurry diluted to a pulp density of about 2.5% solids by weight with barren solution from a gold recovery step. The diluted slurry was thickened, with the under flow being in the 45 to 51% solids range. The gold was recovered from the overflow by carbon adsorption, with subsequent stripping by NaCN/NaOH solution and cementation of gold and silver with zinc dust. The under flow slurry was diluted to about 30%
solids by recycle, and gold was recovered in the carbon in leach step. It was found that about 94.5% of the extract-able gold was recovered from the thickener overflow in the gold recovery step, with the remaining 5.5% being recovered from the thickener under flow in the carbon in leach step.
~23g~9~
Other examples and embodiments will be readily apparent to a person skilled in the art, the scope of the invention being defined in the appended claims.
:
:
Claims (9)
1. A process for recovering gold from refractory auriferous iron-containing sulphidic material comprising:
treating an aqueous slurry of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250°C under a total pressure of from about 500 to about 5000 kPa to oxidize sulphide sulphur to sulphate form and release gold from a refractory state, adjusting the pH of the resultant oxidized slurry to a value suitable for cyanidation, subjecting the pH adjusted slurry to a cyanidation step in which gold is dissolved in a cyanide solution, diluting the cyanided slurry to a pulp density in the range of from about 2 to about 10% solids by weight, subjecting the diluted slurry to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and separately recovering gold from the gold-containing solution and from the high pulp density gold-containing slurry.
treating an aqueous slurry of the material in a pressure oxidation step at a temperature in the range of from about 135 to about 250°C under a total pressure of from about 500 to about 5000 kPa to oxidize sulphide sulphur to sulphate form and release gold from a refractory state, adjusting the pH of the resultant oxidized slurry to a value suitable for cyanidation, subjecting the pH adjusted slurry to a cyanidation step in which gold is dissolved in a cyanide solution, diluting the cyanided slurry to a pulp density in the range of from about 2 to about 10% solids by weight, subjecting the diluted slurry to a liquid-solids separation step to produce a gold containing solution and a relatively high pulp density gold-containing slurry, and separately recovering gold from the gold-containing solution and from the high pulp density gold-containing slurry.
2. A process according to claim 1 including washing the oxidized slurry prior to the pH adjustment step to remove soluble iron, arsenic if present and sulphate.
3. A process according to claim 1 including recover-ing gold from the gold containing solution by adsorption by activated carbon.
4. A process according to claim 1 including removing gold from the gold-containing solution by adsorption by an ion exchange resin.
5. A process according to claim 1 including recovering gold from the high pulp density slurry by adsorption by acti-vated carbon.
6. A process according to claim 1 wherein the rela-tively high pulp density gold-containing slurry has a pulp density in the range of from about 45 to about 60% solids by weight.
7. A process according to claim 1 including diluting the resultant high pulp density slurry to a pulp density of from about 35 to about 45% solids by weight before removing gold therefrom.
8. A process according to claim 1 wherein the pressure oxidation step is carried out at atemperature in the range of from about 160 to about 200°C.
9. A process according to claim 1 wherein the cyanided slurry is diluted by barren solution produced after recovery of gold from the gold-containing solution.
Priority Applications (8)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000464183A CA1234291A (en) | 1984-09-27 | 1984-09-27 | Recovery of gold from auriferous refractory iron- containing sulphidic material |
| US06/707,711 US4610724A (en) | 1984-09-27 | 1985-03-04 | Recovery of gold from refractory auriferous iron-containing sulphidic material |
| GR852305A GR852305B (en) | 1984-09-27 | 1985-09-23 | |
| ZA857337A ZA857337B (en) | 1984-09-27 | 1985-09-24 | Recovery of gold from refractory auriferous iron-containing sulphidic material |
| AU47891/85A AU569175B2 (en) | 1984-09-27 | 1985-09-25 | Pressure leach of refractory auriferous ores prior to cyanidation, activated carbon or ion-exchange resin for gold recovery |
| DE8585306892T DE3577881D1 (en) | 1984-09-27 | 1985-09-27 | GOLD PRODUCTION FROM GOLD-CONTAINING, DIFFICULT-TO-LOCKABLE SULFIDIC MATERIALS WITH AN IRON CONTENT. |
| EP85306892A EP0177294B1 (en) | 1984-09-27 | 1985-09-27 | Recovery of gold from refractory auriferous iron-containing sulphidic material |
| CN85107901A CN1007624B (en) | 1984-09-27 | 1985-10-26 | Recovery of gold from auriferous refractory iron-containing sulphidic ore |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000464183A CA1234291A (en) | 1984-09-27 | 1984-09-27 | Recovery of gold from auriferous refractory iron- containing sulphidic material |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1234291A true CA1234291A (en) | 1988-03-22 |
Family
ID=4128793
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000464183A Expired CA1234291A (en) | 1984-09-27 | 1984-09-27 | Recovery of gold from auriferous refractory iron- containing sulphidic material |
Country Status (7)
| Country | Link |
|---|---|
| US (1) | US4610724A (en) |
| EP (1) | EP0177294B1 (en) |
| AU (1) | AU569175B2 (en) |
| CA (1) | CA1234291A (en) |
| DE (1) | DE3577881D1 (en) |
| GR (1) | GR852305B (en) |
| ZA (1) | ZA857337B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5573575A (en) * | 1993-12-03 | 1996-11-12 | Geobiotics, Inc. | Method for rendering refractory sulfide ores more susceptible to biooxidation |
| US6146444A (en) * | 1993-12-03 | 2000-11-14 | Geobiotics, Inc. | Method for recovering metal value from concentrates of sulfide minerals |
Families Citing this family (27)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3534224A1 (en) * | 1985-09-23 | 1987-04-02 | Gock Eberhard Priv Doz Prof Dr | METHOD FOR THE WET-CHEMICAL EXTRACTION OF PRECIOUS METALS FROM CARBON-CONTAINING ARSENOPYRITE CONCENTRATES |
| US4842644A (en) * | 1986-10-07 | 1989-06-27 | Senff Anthony N | Silver recovery method |
| US4979987A (en) | 1988-07-19 | 1990-12-25 | First Miss Gold, Inc. | Precious metals recovery from refractory carbonate ores |
| MY105658A (en) * | 1989-03-07 | 1994-11-30 | Butler Dean R | Noble metal recovery |
| ES2038535B1 (en) * | 1991-06-14 | 1994-04-01 | Riotinto Minera Sa | PROCEDURE FOR THE HYDROMETALLURGICAL RECOVERY OF NON-IRON METALS IN ASHES OF PIRITAS. |
| CA2054522C (en) * | 1991-10-30 | 2000-08-08 | C. Neil Smith | Ore feed heating |
| US5256189A (en) * | 1992-05-20 | 1993-10-26 | Prime Resources Group Inc. | Aqueous oxidation of sulfidic silver ore |
| US5338338A (en) * | 1992-09-22 | 1994-08-16 | Geobiotics, Inc. | Method for recovering gold and other precious metals from carbonaceous ores |
| US5364453A (en) * | 1992-09-22 | 1994-11-15 | Geobiotics, Inc. | Method for recovering gold and other precious metals from carbonaceous ores |
| US5320720A (en) * | 1993-01-05 | 1994-06-14 | Prime Resources Group Inc. | Extraction of precious metals from ores thereof |
| US5458866A (en) * | 1994-02-14 | 1995-10-17 | Santa Fe Pacific Gold Corporation | Process for preferentially oxidizing sulfides in gold-bearing refractory ores |
| CN1034675C (en) * | 1994-03-25 | 1997-04-23 | 长春黄金研究所 | Quick-cyaniding gold-extracting method in autoclave |
| US5489326A (en) * | 1994-10-04 | 1996-02-06 | Barrick Gold Corporation | Gold recovery using controlled oxygen distribution pressure oxidation |
| US5851499A (en) * | 1996-09-11 | 1998-12-22 | Newmont Gold Company | Method for pressure oxidizing gold-bearing refractory sulfide ores having organic carbon |
| US6368381B1 (en) | 1998-03-11 | 2002-04-09 | Placer Dome Technical Services, Ltd. | Autoclave using agitator and sparge tube to provide high oxygen transfer rate to metal-containing solutions |
| US7604783B2 (en) | 2004-12-22 | 2009-10-20 | Placer Dome Technical Services Limited | Reduction of lime consumption when treating refractor gold ores or concentrates |
| US8061888B2 (en) | 2006-03-17 | 2011-11-22 | Barrick Gold Corporation | Autoclave with underflow dividers |
| US8252254B2 (en) | 2006-06-15 | 2012-08-28 | Barrick Gold Corporation | Process for reduced alkali consumption in the recovery of silver |
| US7691346B2 (en) * | 2007-06-19 | 2010-04-06 | Chemical Lime Company | Process for recausticizing cyanide leach solutions |
| AU2008300274B2 (en) * | 2007-09-18 | 2012-04-19 | Barrick Gold Corporation | Process for mercury control during pressure oxidation |
| RU2514900C2 (en) * | 2012-07-04 | 2014-05-10 | Общество с ограниченной ответственностью "Научно-иследовательский центр "Гидрометаллургия" | Processing of gold-bearing concentrates of two-fold hardness |
| RU2552217C1 (en) * | 2014-04-04 | 2015-06-10 | Общество с ограниченной ответственностью "Научно-исследовательский центр "Гидрометаллургия" | Processing of gold-bearing concentrates of two-fold hardness |
| EA026707B1 (en) * | 2015-01-22 | 2017-05-31 | Открытое Акционерное Общество "Иркутский Научно-Исследовательский Институт Благородных И Редких Металлов И Алмазов", Оао "Иргиредмет" | Method of extracting precious metals from refractory sulphide raw stock |
| RU2627835C2 (en) * | 2016-01-12 | 2017-08-11 | Общество с ограниченной ответственностью "Комплексные технологии" | Method of complex processing of pyritic raw materials |
| RU2636775C2 (en) * | 2016-02-20 | 2017-11-28 | Общество с ограниченной ответственностью "Научно-исследовательский центр "Гидрометаллургия" | Two-fold hardness gold-bearing concentrates processing method |
| RU2629125C1 (en) * | 2016-11-25 | 2017-08-24 | Общество с ограниченной ответственностью "Научно-исследовательский центр "Гидрометаллургия" | Method of processing gold-containing concentrates of double holding |
| EA035804B1 (en) * | 2017-08-11 | 2020-08-13 | Акционерное Общество "Полиметалл Инжиниринг" | Method of gold extraction from double refractory concentrates |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2777764A (en) * | 1954-07-09 | 1957-01-15 | American Cyanamid Co | Process of recovering precious metals from refractory source materials |
| US4038362A (en) * | 1976-11-04 | 1977-07-26 | Newmont Explorations Limited | Increasing the recoverability of gold from carbonaceous gold-bearing ores |
| CA1106617A (en) * | 1978-10-30 | 1981-08-11 | Grigori S. Victorovich | Autoclave oxidation leaching of sulfide materials containing copper, nickel and/or cobalt |
| ES476055A1 (en) * | 1978-12-15 | 1979-11-01 | Redondo Abad Angel Luis | Process for non-ferrous metals production from complex sulphide ores containing copper, lead, zinc, silver and/or gold |
-
1984
- 1984-09-27 CA CA000464183A patent/CA1234291A/en not_active Expired
-
1985
- 1985-03-04 US US06/707,711 patent/US4610724A/en not_active Expired - Lifetime
- 1985-09-23 GR GR852305A patent/GR852305B/el unknown
- 1985-09-24 ZA ZA857337A patent/ZA857337B/en unknown
- 1985-09-25 AU AU47891/85A patent/AU569175B2/en not_active Ceased
- 1985-09-27 EP EP85306892A patent/EP0177294B1/en not_active Expired - Lifetime
- 1985-09-27 DE DE8585306892T patent/DE3577881D1/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5573575A (en) * | 1993-12-03 | 1996-11-12 | Geobiotics, Inc. | Method for rendering refractory sulfide ores more susceptible to biooxidation |
| US6146444A (en) * | 1993-12-03 | 2000-11-14 | Geobiotics, Inc. | Method for recovering metal value from concentrates of sulfide minerals |
| US6387155B1 (en) | 1993-12-03 | 2002-05-14 | Geobiotics, Llc | Method for recovering metal values from concentrates of sulfide minerals |
| US6652622B2 (en) | 1993-12-03 | 2003-11-25 | Geobiotics, Llc. | Method for recovering metal values from concentrates of sulfide minerals |
| US7156894B2 (en) | 1993-12-03 | 2007-01-02 | Geobiotics, Llc | Method for recovering metal values from concentrates of sulfide minerals |
| US7429286B2 (en) | 1993-12-03 | 2008-09-30 | Geobiotics, Llc | Method for recovering metal values from concentrates of sulfide minerals |
| US8029598B2 (en) | 1993-12-03 | 2011-10-04 | Geobiotics, Llc | Method for recovering metal values from refractory sulfide ore |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0177294A3 (en) | 1988-05-11 |
| AU4789185A (en) | 1986-04-10 |
| EP0177294B1 (en) | 1990-05-23 |
| ZA857337B (en) | 1986-05-28 |
| US4610724A (en) | 1986-09-09 |
| DE3577881D1 (en) | 1990-06-28 |
| GR852305B (en) | 1986-01-17 |
| AU569175B2 (en) | 1988-01-21 |
| EP0177294A2 (en) | 1986-04-09 |
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